[go: up one dir, main page]

EP0799799A1 - Verfahren und Vorrichtung zur Reinigung proteinhaltiger Abwässer - Google Patents

Verfahren und Vorrichtung zur Reinigung proteinhaltiger Abwässer Download PDF

Info

Publication number
EP0799799A1
EP0799799A1 EP19970200993 EP97200993A EP0799799A1 EP 0799799 A1 EP0799799 A1 EP 0799799A1 EP 19970200993 EP19970200993 EP 19970200993 EP 97200993 A EP97200993 A EP 97200993A EP 0799799 A1 EP0799799 A1 EP 0799799A1
Authority
EP
European Patent Office
Prior art keywords
waste water
tank
protein containing
line
purified
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP19970200993
Other languages
English (en)
French (fr)
Other versions
EP0799799B1 (de
Inventor
Jelle Van Der Spoel
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
FrieslandCampina Nederland BV
Original Assignee
FrieslandCampina Germany GmbH
Verenigde Cooperatieve Melkindustrie "coberco" Ba
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by FrieslandCampina Germany GmbH, Verenigde Cooperatieve Melkindustrie "coberco" Ba filed Critical FrieslandCampina Germany GmbH
Publication of EP0799799A1 publication Critical patent/EP0799799A1/de
Application granted granted Critical
Publication of EP0799799B1 publication Critical patent/EP0799799B1/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
    • A23J1/16—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from waste water of starch-manufacturing plant or like wastes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the invention relates to a method for purifying protein containing waste water, in which (a) a first insoluble protein containing material is caused to form in the waste water, (b) the mixture obtained in step (a) is separated to form pre-purified waste water, (c) the pre-purified waste water is treated with aerobic microorganisms and (d) the mixture obtained in step (c) is separated to form finely purified waste water.
  • the invention also relates to a device for purifying protein containing waste water.
  • WO 92/19547 describes a method and device for purifying waste water containing carbohydrates, proteins and fats.
  • waste water is fed in a first step to a first aeration tank which contains microorganisms.
  • a cationic and/or an anionic polymer and possibly a solution of an iron(III) salt in water is fed to the waste water to make some of the microorganisms flocculate and to remove phosphate.
  • the waste water is then fed to a flotation device, where it is separated into flotation sludge and a first effluent.
  • the first effluent is then fed to a second aeration tank which also contains microorganisms and is provided with a separating device.
  • the first effluent is purified to form purification sludge and a second effluent. Some of the purification sludge is then fed back to the first aeration tank and another portion is fed back to the second aeration tank.
  • the method and the device are suitable, in particular, for purifying waste water originating from a foodstuffs processing factory.
  • Both the first and the second purification step comprise a biological purification with the aid of microorganisms. Because, in particular, the biological purification in the first step requires a large amount of oxygen, the energy consumption is high in the first step. If sufficient oxygen cannot be fed to the device, for example if the waste water to be purified contains a large amount of impurities, a strong stench due to rotting may be produced, which is disadvantageous for the immediate dwelling and working environment of the device. The purification sludge as such is also no longer directly usable, for example in agriculture or as an additive for livestock fodders.
  • One more disadvantage of the device according to WO 92/19547 is that the device must be operated for an expedient employment on a relatively large scale, which not only imposes a load on the available space, but also requires large investment.
  • the present invention provides a solution to the problems described above.
  • the invention therefore provides a method and a device as stated in the introduction, in which proteins and other constituents, such as fats and carbohydrates, are removed from waste water in a very expedient way.
  • a purification sludge is also obtained which has much nutritive value for livestock and which can therefore be used preeminently as an additive to livestock fodders.
  • phosphate which is present in the waste water, is also removed to a large extent from the waste water.
  • a further advantage of the invention is that there is no risk of the occurrence of stench.
  • the scale of the device can be relatively small. The invention therefore relates to a method as stated in the preamble, in which step (b) and step (d) are carried out in the same device.
  • step (b) and (d) are therefore preferably also carried out alternately in the same device.
  • step (a) is carried out batchwise, that is to say that the steps (a) - (d) are carried out in the sequence specified and not simultaneously.
  • step (a) can indeed be carried out during the carrying out of step (b), (c) or (d) using another batch of waste water.
  • this will be a more expedient implementation of the method according to the invention.
  • step (a) is therefore carried out during steps (b) and/or (c) and/or (d).
  • Waste water in particular waste water from foodstuffs- and milk-processing industries, contains, inter alia, proteins, carbohydrates and fats. It has been found that essentially the proteins and the fats are advantageously removed from the waste water in a first step and the other constituents, generally carbohydrates, are then removed in a second step. To remove proteins, it is necessary for the pH of the waste water to be adjusted to a correct value for causing a first insoluble protein containing material to form.
  • the term "insoluble” is understood here as meaning that, although a small amount of the protein containing material may be present in the waste water in dissolved form, most of the material is precipitated.
  • the pH of the waste water is preferably adjusted in such a way that the proteins present in the waste water coagulate and/or flocculate. It is, however, possible that some of the proteins are already present in undissolved form. According to the invention, the pH of the waste water is therefore adjusted during step (a) to a value which is preferably in the region of the coagulation point of the proteins.
  • Coagulation is understood to mean a chemical process in which colloidal particles, such as proteins, which are present in the waste water, agglomerate to form larger particles as a result of adding materials which interact with the colloidal particles. The consequence of said interaction is that the colloidal particles agglomerate to form larger agglomerates which readily settle.
  • Flocculation is a physico-chemical process, in which agglomerates of colloidal particles are formed by mutually forming bridges between the colloidal particles or by neutralizing the charge of the colloidal particles.
  • the pH of the waste water is advantageously adjusted during step (a) to a value at which a first protein containing material precipitates.
  • the adjustment of the pH is carried out by adding an acid or a base to the waste water.
  • Suitable acids are inorganic acids, for example sulphuric acid, nitric acid and hydrochloric acid, and organic acids, for example acetic acid and formic acid.
  • Suitable bases are primarily inorganic bases, for example potassium hydroxide, sodium hydroxide and ammonium hydroxide.
  • an inorganic acid, in particular nitric acid is used as acid and an inorganic base, in particular sodium hydroxide, is used as base.
  • the pH is preferably adjusted to a value of 7 - 10 and, in particular, to a value of 8.5 - 9.5.
  • a first coagulating material should be added, in which connection the first coagulating material may be an anionic or a cationic polymer or a combination of an anionic and a cationic polymer. It has been found, however, that the coagulating material is advantageously an anionic polymer.
  • an anionic polymer preferably a strongly anionic polymer suitable for consumption in certain quantities, and in particular the anionic polymer "Supervlok A150" which is marketed by the company Cytec Industries B.V., is therefore added prior to step (b).
  • This anionic polymer is a copolymer of acrylamides of which some are anionically active.
  • the amount of anionic polymer which is added depends strongly on the degree of contamination, in particular the contamination in the form of proteins and fats, of the waste water. It will be clear to the person skilled in the art that more anionic polymer will have to be added as the level of contamination of the waste water increases. However, an amount of approximately 1 - 100 ppm, relative to the amount of waste water, will often be added and preferably an amount of 5 - 20 ppm of the anionic polymer will be added.
  • a solution of a metal salt in water may also be added because the presence of a metal salt in the waste water promotes the coagulation and/or flocculation of the proteins and fats and the removal of phosphate.
  • a solution of iron(III) chloride or of aluminium(III) chloride in water is added.
  • phosphate is also removed. It has been found that the phosphate is removed from the waste water essentially in the form of calcium phosphate because it is entrapped by the larger agglomerates of the proteins and fats.
  • the proteins, fats and phosphate, in particular calcium phosphate are preferably essentially removed from the waste water during steps (a) and (b), and the other constituents, in particular the carbohydrates, are removed during steps (c) and (d).
  • a second coagulating material may be an anionic or a cationic polymer or a combination of an anionic and a cationic polymer.
  • the second coagulating material is preferably a cationic polymer, more preferably a strongly cationic polymer which is suitable for consumption in certain amounts and, in particular, the cationic polymer "C496", which is marketed by the company Cytec Industries B.V.. Said cationic polymer is a copolymer of acrylamides, some of which are cationically active.
  • the second coagulating material is preferably added after adding the first coagulating material. According to the invention, an amount of a cationic polymer is therefore added after step (c).
  • the amount of the cationic polymer which is added depends strongly on the degree of contamination, in particular the contamination in the form of proteins and fats, of the waste water. It will be clear to the person skilled in the art that more cationic polymer will have to be added as the level of contamination of the waste water increases. However, an amount of approximately 1 - 100 ppm, relative to the amount of waste water, and preferably an amount of 5 - 20 ppm of the cationic polymer will often be added.
  • the purification is preferably carried out at a temperature of approximately 5 - 45°C, in particular at a temperature of 20 - 40°C.
  • the invention also relates to a device for purifying protein containing waste water.
  • the device comprises a first tank which is connected to a flotation device.
  • the flotation device is also connected to a second tank in which microorganisms are present.
  • a preferred embodiment of said device is shown in the figure.
  • Said embodiment comprises a tank 1 which is provided with feed lines 4 - 6 and drainage line 9.
  • Tank 1 also has means 7 and 8 for registering the liquid level in tank 1 and for measuring the pH of the liquid in tank 1, respectively.
  • the preferred embodiment further comprises a flotation device 2 which is connected to tank 1 by line 9.
  • the flotation device is provided with feed line 10 and drainage lines 11 - 13.
  • the preferred embodiment furthermore comprises a tank 3 which is connected to the flotation device 2 by lines 13 and 16.
  • Tank 3 is provided with feed lines 14 and 15 and drainage line 16.
  • at least lines 9 and 13 are provided with pumps 17 and 18.
  • the device also comprises a process control system.
  • the device is preferably operated as follows.
  • Tank 1 is filled via feed line 4 with the protein containing waste water to be purified.
  • the acid is added via feed line 5 or the base via feed line 6 to adjust to the desired pH.
  • the pH is measured by means 8 which is connected to the process control system which regulates whether acid or base has to be added and which regulates the amount thereof which is necessary for adjusting to the desired pH.
  • the reaching of a certain liquid level in tank 1 is measured using means 7 which is also connected to the process control system.
  • tank 1 is emptied, for example to approximately 20% of the total volume. The supply of the waste water to be purified and the adjustment of the pH are maintained.
  • waste water in tank 1 has the desired pH, formation of a first insoluble protein containing material occurs.
  • the mixture of waste water and the first insoluble protein containing material is fed by means of pump 17 to the flotation device via line 9. Once the mixture has been fed to the flotation device, the pump 17 is stopped at a low-level message signal by means 7.
  • the desired amount of the anionic polymer is then added via line 10.
  • the anionic polymer can also be added before the mixture has reached the flotation device, but it must, however, take place after the mixture has left tank 1.
  • Line 10 can therefore also be placed, for example, between pump 17 and the feed point of the flotation device 2.
  • the coagulated and/or flocculated particles come into contact with air, in which process a foam is formed.
  • said foam is separated from the waste water by means of a scraper.
  • the mixture of the waste water and the first insoluble protein containing polymer is separated into a pre-purified waste water and a protein containing sludge.
  • the protein containing sludge is drained via line 12, while the pre-purified waste water is fed by means of pump 18 via line 13 to tank 3.
  • Air is fed into tank 3 via supply line 15. This aeration is preferably carried out for at least 4 hours.
  • the desired amount of cationic polymer is fed via supply line 14 into line 16, upstream of flotation device 2.
  • the effluent from tank 3 is fed via line 16 to the flotation device 2 in such a way that the cationic polymer is fed at the same point as that of the feed of the anionic polymer.
  • Line 16 therefore preferably comes out at the same feed point of the flotation device 2 as that of line 10 while line 14 is preferably immediately upstream of said fuel point.
  • the effluent is fed via line 16 to the flotation device.
  • the effluent is then floated to form finely purified waste water which is drained via line 11.
  • the second insoluble material is drained via line 12.
  • the device may optionally be provided with more means for feeding through the various process streams, for example conveyor belts, pumps and stirring devices.
  • Another advantage of the method according to the invention is that fats and proteins are removed in the first stage, that is to say during steps (a) and (b). There is therefore scarcely a risk of stench nuisance (mercaptans) occurring during the decomposition of carbohydrates in tank 3.
  • phosphate is removed during the steps (a) and (b). There is therefore also no risk of the microorganisms present in tank 3 being deactivated by calcification because, as a result of the reduced pH in tank 3, calcium phosphate and, as a result of the presence of carbon dioxide, calcium carbonate can precipitate.
  • the flotation device can optionally be provided with a separate line for draining the second insoluble material.
  • the first insoluble material and the second insoluble material can also be drained via the same line, but to separate storage points.
  • tank 3 is provided with an additional direct drainage line 19.
  • the feeding of air to tank 3 is stopped by means 7 and the process control system.
  • the aeration in tank 3 is stopped when tank 1 is partly filled, in particular is filled to approximately 60% of the total volume.
  • the second insoluble material can then settle in tank 3. After purification in tank 3, most of the finely purified water can be drained via said additional line 19. The second insoluble material is fed together with the small residual amount of the finely purified waste water to flotation device 2.
  • tank 1 is filled further to approximately the maximum volume, the time duration between the filling of tank 1 from approximately 60% of the total volume to approximately the maximum volume being approximately equal to that which is necessary to settle the second insoluble material, to drain most of the finely purified waste water via line 19 and to feed the second insoluble material and the small residual amount of the finely purified waste water to the flotation device 2.
  • line 16 is connected to tank 3 in such a way that a level difference is present between line 16 and the bottom of tank 3, with the result that, when the second insoluble material and the small residual amount of the finely purified waste water are fed to the flotation device 2, a small portion of the second insoluble material remains behind in tank 3 for the purpose of purifying a subsequent charge of pre-purified waste water.
  • Tank 1 is then emptied with the aid of pump 17 to approximately 20% of the total volume, preferably at a flow rate higher than that at which tank 1 is filled with waste water.
  • pump 18 ensures that tank 3 is filled with pre-purified waste water at a flow rate which is preferably approximately equal to that with which tank 1 is emptied.
  • the device therefore comprises at least one tank 1, a flotation device 2 and a tank 3, and the further means, pumps and lines 4 - 19, tank 3 being connected to flotation device 2 by means of line 16 and lines 9 and 13 comprising pumps 17 and 18.
  • a method according to the invention which comprises only the steps (a) and (b) and a device which is suitable for carrying out the steps (a) and (b).
  • the method then comprises (a) making an insoluble protein containing material form and (b) separating the mixture obtained in step (a) to form purified waste water, in which process, during step (a), the pH of the waste water is adjusted to a value of 7 - 10 and preferably an amount of an anionic polymer is added prior step (b).
  • the exceptional expediency of such a method is that in general at least 80% and usually even more than 90% of the proteins and fats are removed during the steps (a) and (b).
  • the pH correction is performed in such a way that the pH of the waste water is increased by at least 0.3 during step (a), preferably by at least 0.5. If the pH of the waste water is in the range of 7-8, the pH adjustment needs to be about 0.5, whereas the pH of the waste water is in the range of 8-9, the pH correction may be about 0.3. However, if the pH of the waste water is above about 9.5, the pH needs to be decreased to a value of about 7.5 and then increased to a pH of about 8. Consequently, it is in general only necessary to increase the pH of the waste water by only a relatively small value, i.e.
  • a suitable device will then comprise a tank (1) and a flotation device (2), tank (1) being provided with feed lines and drainage lines (4) - (6) and (9) and means (7) and (8) for registering the liquid level and for adjusting the pH of the liquid in tank (1), respectively, the flotation device (2) being connected by line (9) to tank (1) and being provided with feed lines and drainage lines (10) - (13), at least line (9) being provided with a pump (17) and a process control system.
  • the method and the device according to the invention are primarily suitable for purifying waste water from a foodstuffs processing factory.
  • a factory of this type are milk-processing factories and creameries.
  • the method and the device according to the invention are suitable, in particular, for purifying waste water from a cheese factory, i.e. waste water originating from the preparation of cheese.
  • the method and the device according to the invention can also be used if the purification in tank 1 is carried out at a pH of less than 7.
  • This has, however, the disadvantage that the pre-purified waste water has first to be neutralized with a base before it is fed to tank 3.
  • the pH has to be kept at a value of approximately 7 by adding base.
  • no phosphate will be removed in tank 1 because of the acidic pH. If the pre-purified waste water still containing phosphate is brought into contact with a base in or upstream of tank 3, there is a risk that phosphate and possibly carbonate may precipitate, which may give rise to calcification of the microorganisms present in tank 3.

Landscapes

  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Microbiology (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Biochemistry (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Inorganic Chemistry (AREA)
  • Separation Of Suspended Particles By Flocculating Agents (AREA)
  • Peptides Or Proteins (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
EP19970200993 1996-04-04 1997-04-04 Verfahren zur Reinigung proteinhaltiger Abwässer Expired - Lifetime EP0799799B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NL1002797 1996-04-04
NL1002797A NL1002797C2 (nl) 1996-04-04 1996-04-04 Werkwijze en inrichting voor het zuiveren van eiwithoudend afvalwater.

Publications (2)

Publication Number Publication Date
EP0799799A1 true EP0799799A1 (de) 1997-10-08
EP0799799B1 EP0799799B1 (de) 2002-02-27

Family

ID=19762626

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19970200993 Expired - Lifetime EP0799799B1 (de) 1996-04-04 1997-04-04 Verfahren zur Reinigung proteinhaltiger Abwässer

Country Status (8)

Country Link
US (1) US6251277B1 (de)
EP (1) EP0799799B1 (de)
AT (1) ATE213718T1 (de)
AU (1) AU728622B2 (de)
CA (1) CA2201835A1 (de)
DE (1) DE69710628T2 (de)
NL (1) NL1002797C2 (de)
NZ (1) NZ314516A (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006115422A1 (en) * 2005-04-28 2006-11-02 Fonterra Co-Operative Group Limited Dairy product and process

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6409927B1 (en) * 1998-06-03 2002-06-25 Enrique-Ruben Cardenas-Granguillhome Process for the treatment of polluted metal-mechanic industrial wastewater and urban water
KR100419430B1 (ko) * 2002-01-05 2004-02-18 삼성엔지니어링 주식회사 단백질 성분 함유 폐수를 처리할 수 있는브레분디모나스속 미생물 및 상기 미생물을 이용한폐수처리 방법
US20050061750A1 (en) * 2003-09-23 2005-03-24 Polymer Ventures, Inc. Methods for the purification of contaminated waters
US20090294381A1 (en) * 2005-07-15 2009-12-03 Zodiac Pool Care, Inc. Methods for controlling ph in water sanitized by chemical or electrolytic chlorination

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3898160A (en) * 1972-07-25 1975-08-05 Us Agriculture Recovering proteins from waste water
GB1512481A (en) * 1977-02-16 1978-06-01 Hartley Simon Ltd Process for removal of proteinaceous matter from liquid effluents
WO1986000788A1 (en) * 1984-07-23 1986-02-13 San Basilio S.R.L. Separation process with recovery of proteins and fats from substances of animal origin, organic substances or refluent from working organic substances and a plant to carry out the process
FR2648309A1 (fr) * 1989-06-16 1990-12-21 So Ge Val Sa Procede de traitement des lisiers de porcherie ainsi qu'installation permettant la mise en oeuvre de ce procede
WO1992019547A1 (en) * 1991-05-01 1992-11-12 Level Valley Dairy Company Wastewater treatment system

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3313795A (en) * 1965-03-01 1967-04-11 Purac Ab Method of treating a liquid containing dissolved proteinaceous constituents
US3444076A (en) * 1965-10-20 1969-05-13 Kurita Industrial Co Ltd Method of treating organic waste water
US4061568A (en) * 1973-02-09 1977-12-06 A/S Apothekernes Laboratorium For Specialpraeparater Method for recovering and stabilizing fat and fatty substances as well as proteins and proteinous substances from process water
US3969203A (en) * 1974-02-19 1976-07-13 Swift & Company Waste water treatment
US3959131A (en) * 1974-10-17 1976-05-25 Swift & Company Apparatus and method for removing pollutants from wastewater
US4001114A (en) * 1975-05-19 1977-01-04 Scm Corporation Waste water treatment process
US4340487A (en) * 1980-12-24 1982-07-20 Lyon Michael R Process for purifying water
NL8204829A (nl) * 1982-12-14 1984-07-02 Schneider & Schuurman Werkwijze en inrichting voor het zuiveren van afvalwater.
US4828577A (en) * 1984-12-03 1989-05-09 Markham Jr William M Process for converting food sludges to biomass fuels
US4728517A (en) * 1984-12-03 1988-03-01 Markham William M Conversion of biological sludge and primary float sludge to animal protein supplement
US4933087A (en) * 1988-12-23 1990-06-12 Markham Jr William M Recovery of fats and proteins from food processing wastewaters with alginates
DK610189D0 (da) * 1989-12-04 1989-12-04 Akvagad A S Fremgangsmaade til rensning af spildevand under anvendelse af flotation og apparat til udoevelse af denne fremgangsmaade
US5514282A (en) * 1994-04-01 1996-05-07 Hibbard; David C. Food processing wastewater treatment and recovery process
US5540836A (en) * 1994-06-16 1996-07-30 Coyne; Thomas J. Wastewater treatment system and method

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3898160A (en) * 1972-07-25 1975-08-05 Us Agriculture Recovering proteins from waste water
GB1512481A (en) * 1977-02-16 1978-06-01 Hartley Simon Ltd Process for removal of proteinaceous matter from liquid effluents
WO1986000788A1 (en) * 1984-07-23 1986-02-13 San Basilio S.R.L. Separation process with recovery of proteins and fats from substances of animal origin, organic substances or refluent from working organic substances and a plant to carry out the process
FR2648309A1 (fr) * 1989-06-16 1990-12-21 So Ge Val Sa Procede de traitement des lisiers de porcherie ainsi qu'installation permettant la mise en oeuvre de ce procede
WO1992019547A1 (en) * 1991-05-01 1992-11-12 Level Valley Dairy Company Wastewater treatment system

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2006115422A1 (en) * 2005-04-28 2006-11-02 Fonterra Co-Operative Group Limited Dairy product and process
AU2006235865B2 (en) * 2005-04-28 2010-07-15 Fonterra Co-Operative Group Limited Dairy product and process

Also Published As

Publication number Publication date
AU728622B2 (en) 2001-01-11
NL1002797C2 (nl) 1997-10-07
DE69710628T2 (de) 2002-11-21
ATE213718T1 (de) 2002-03-15
US6251277B1 (en) 2001-06-26
CA2201835A1 (en) 1997-10-04
AU1773797A (en) 1997-10-09
NZ314516A (en) 2000-01-28
EP0799799B1 (de) 2002-02-27
DE69710628D1 (de) 2002-04-04

Similar Documents

Publication Publication Date Title
US8147695B2 (en) Method of removing phosphorus from wastewater
US4013555A (en) Process for reducing BOD in food processing plant wastes
US4208282A (en) Process for the purification of sewage while recapturing the fatty and albuminous matter in reusable form
US4670158A (en) Primary treatment of wastewater
US6251277B1 (en) Method and device for purifying protein containing waste water
CA2227333A1 (en) Method and apparatus for waste water treatment
JP3805963B2 (ja) 生物由来有機性廃棄物の処理方法およびその装置
KR940006408B1 (ko) 활성화 슬러지의 증량 방지방법
EP0765292B1 (de) Verfahren zum säubern von molkereispülwasser
JPH10202271A (ja) フッ素、リン酸及び有機物含有廃水の処理方法
JP3457013B2 (ja) フッ化物イオン含有排水の処理方法
JPH0230320B2 (de)
JP2861371B2 (ja) 排水処理法
KR20010009316A (ko) 돈 분뇨 정화처리장치
JP3547113B2 (ja) 廃牛乳の処理方法
US4228003A (en) Method of removing phosphates from waste water
JPH0732913B2 (ja) 廃水処理装置
JP2957464B2 (ja) 過酸化水素含有排水の処理方法
US20210355004A1 (en) Method for dewatering or removing solids, including corn solids, via flocculation from an alkaline aqueous solution, including nejayote, generated in the process of nixtamalization of corn by introducing a source of carbonate to the aqueous solution, followed by adding an anionic and then a cationic flocculent to the aqueous solution.
JPH0228388B2 (de)
JP3420777B2 (ja) アルミニウムの不溶化方法
EP0066417B1 (de) Verfahren zum Klären von Protein-Abwasser, das feste Verunreinigungen enthält
JP2001070951A (ja) リン含有水の処理方法
JP2005169268A (ja) 余剰汚泥の処理装置および処理方法
JPS6246240B2 (de)

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE

17P Request for examination filed

Effective date: 19970903

17Q First examination report despatched

Effective date: 19990302

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: ZUIVELCOOEPERATIE DE ZEVEN PROVINCIEN U.A.

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: FRIESLAND COBERCO DAIRY FOODS HOLDING N.V.

RAP1 Party data changed (applicant data changed or rights of an application transferred)

Owner name: FRIESLAND BRANDS B.V.

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

RTI1 Title (correction)

Free format text: METHOD FOR PURIFYING PROTEIN CONTAINING WASTE WATER

GRAG Despatch of communication of intention to grant

Free format text: ORIGINAL CODE: EPIDOS AGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

GRAH Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOS IGRA

REG Reference to a national code

Ref country code: GB

Ref legal event code: IF02

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AT BE CH DE DK ES FI FR GB GR IE IT LI LU MC NL PT SE

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020227

Ref country code: LI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020227

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED.

Effective date: 20020227

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020227

Ref country code: FR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020227

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020227

Ref country code: CH

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020227

Ref country code: AT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020227

REF Corresponds to:

Ref document number: 213718

Country of ref document: AT

Date of ref document: 20020315

Kind code of ref document: T

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20020404

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20020404

REF Corresponds to:

Ref document number: 69710628

Country of ref document: DE

Date of ref document: 20020404

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 20020430

Year of fee payment: 6

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020527

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020527

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020527

NLV1 Nl: lapsed or annulled due to failure to fulfill the requirements of art. 29p and 29m of the patents act
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20020829

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

EN Fr: translation not filed
PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: IE

Payment date: 20030120

Year of fee payment: 7

26N No opposition filed

Effective date: 20021128

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 20030325

Year of fee payment: 7

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 20030418

Year of fee payment: 7

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20030505

Year of fee payment: 7

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040404

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040405

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20040430

BERE Be: lapsed

Owner name: *FRIESLAND BRANDS B.V.

Effective date: 20040430

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20041103

GBPC Gb: european patent ceased through non-payment of renewal fee
REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A